A HIGH PRODUCTIVE PROCESS FOR PRODUCTION OF LOWER OLEFINS BY CATALYTIC CONVERSION

Abstract: A process for producing light olefins, especially ethylene, propylene,isobutylene and isoamylene, together with high octane gasoline as by-product, comprises that petroleum hydrocarbons are contacted with phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts and catalytically converted at a temperature of 480° to 680° C and a pressure of 1.2×10 5 to 4.0×10 5 Pa, with a contact time of 0.1 to 6 seconds, a weight ratio of catalyst to feedstock of 4:1 to 20:1 and a weight ratio of steam to feedstock of 0.01:1 to 0.5:1.

Description: Field of the Invention The present invention relates to a process of catalytic conversion of petroleum hydrocarbons, and most particularly to a process for producing light olefins, especially ethylene, propylene, isobutylene and isoamylene together with high octane gasoline as by-product by catalytic conversion of petroleum hydrocarbons using phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts. Description of the Prior Art The light olefins can be produced from petroleum hydrocarbons. Their production methods include tubular furnace pyrolysis by using light natural gas, naphtha or light gas oil as feedstocks, thermal cracking over heat carrier by using heavy hydrocarbons as feedstocks, and catalytic conversion of lower aliphatic alcohol as feedstocks. The conventional catalytic cracking also produces light olefins as by-products with a yield of only less than 15% by weight of feedstock during the production of gasoline and light cycle oil. Recently,investigations for catalysts which are more effective for converting petroleum hydrocarbons to light olefins have been made and the result of the investigations has been reported in various patents. The production of light olefins using oxides supported metal catalysts, wherein the support can be SiO 2 , Al 2 O 3 , or other oxides and the metal components are mainly selected from elements of IIB, VB, VIIB, and VIII groups, as disclosed in U.S. Pat.Nos.3,541,179 and 3,647,68Z;D.D.NO.225,135 and S.U.NO.1,214,726. As the supported metal possesses dehydrogenation ability, it accelerates the aromatics condensation and coke formation reaction during the cracking reaction process. Hence, these types o f catalysts can only be used for processing light hydrocarbons. Potassium vanadate, potassium stannate, or potassium niobate is used as catalyst for cracking gasoline to obtain approximately 56% by weight of C 2 -C 4 olefins, wherein ethylene yield is 36.5% by weight and propylene yield is 12.5% by weight, as disclosed in S.U.Nos.523,133, 487,927 and 410,073. D.D.No.152,356 discloses a method for producing light olefins by cracking of various liquid hydrocarbons or hydrocarbon fractions including gasoline, kerosene, gas oil, or vacuum distillates, by a fixed or moving bed reactor, using amorphous silica-alumina catalysts at a temperature of f 600° to 800° C and a contact time of 0.3 to 0.7 seconds, with C 2 -C 4 olefins yield of 40-55% by weight. JP 60-222,428 discloses a process using ZSM-5 zeolite as catalyst and C 5 -C 25 paraffinic hydrocarbons as feedstocks. The process is carried out at a temperature of 600° to 750° C and a weight space velocity of 20 to 300 per hour, with a C 2 -C 4 olefins yield of roughly 30% by weight. These above processes involve high cracking temperature, and hydrocarbon feedstocks which are limited by relatively narrow boiling ranges. U.S.Pat.No.3,758,403 discloses a method using mixed ZSM-5 zeolite and REY zeolite as catalyst, under catalytic cracking conditions to enhance the octane number and yield of gasoline product and obtain higher light olefins yield than that of using single REY zeolite as catalyst. In the example of said patent, vacuum gas oil boiling range from 220° to 510° C is used as feedstock, and is dealt with at the temperature of about 483° C, the volume space velocity of 4 per hour and catalyst-to-feedstock ratio of 1.5 : 1, to obtain yields of 10∼15% by weight for propylene and butylene. In U.S.Pat.No.4,980,053 and EP.No.305,720A, the present applicants disclose a process for the production of f light olefins by cracking of petroleum hydrocarbons including gasoline, kerosene, vacuum gas oil, or residual oil in a fluidized or moving bed or dense phase transfer line reactor using mixed ZSM-5 zeolite and Y zeolite as catalyst at a temperature of 500° to 650° C, with a weight space velocity of 0.2 to 20 per hour and catalyst-to-feedstock ratio of 2:1 to 12:1, to obtain a C 2 -C 4 olefins yield of about 40% by weight. In CN No.1072203 A, the present applicants also disclose a process for producing LPG and high octane gasoline by cracking of petroleum hydrocarbons including gasoline, kerosene, vacuum gas oil, or residual oil in a riser or fluidized bed reactor using ZSM-5 zeolite, high silica Y zeolite and KEY zeolite as catalyst at a temperature of 480° to 550° C, with a weight space velocity of 1 to 150 per hour and catalyst-to-feedstock ratio of 4:1 to 15:1, to obtain a propylene and butylene yield of 20∼30% by weight. The object of the present invention is to provide a catalytic conversion process for producing light olefins, especially ethylene, propylene, isobutylene, and isoamylene togetber with high octane gasoline as by-product from petroleum hydrocarbons in riser or downflow transfer line reactor or fluidized bed reactor, using phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts under given operating conditions. Other objects of the present invention can be learned from the content of the specification of the present invention including the claims. Summary of the Invention A process for producing light olefins, especially ethylene, propylene, isobutylene and isoamylene together with high octane gasoline as by-product, by catalytic conversion of petroleum hydrocarbons comprises contacting the petroleum hydrocarbons with phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts in a moving catalyst reactor and reacting at a temperature of 480° to 680° C and a pressure of 1.2×10 5 to 4.0×10 5 Pa, with a contact time of 0.1 to 6 seconds, a weight ratio of catalyst to feedstock of 4:1 to 20:1 and a weight ratio of steam to feedstock of 0.01:1 to 0.5:1. The reaction effluent is separated to obtain light olefins and liquid products, the spent catalyst is stripped and then removed to a regenerator where it is contacted with an oxygen containing gas at a temperature of 600° to 800° C and is regenerated, the regenerated catalyst is stripped and then recycled to the reactor for reuse. Detailed Description of the Invention The step of the process provided by the present invention is as follows: preheated hydrocarbon feedstocks are contacted with hot phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts in the riser or downflow transfer line reactor or fluidized bed reactor and catalytically converted under given operating conditions. The reaction effluent, steam and spent catalyst are separated by rapid gas-solid separation, the reaction effluent is continuously separated to obtain light olefins and liquid products, and the spent catalyst is continuously removed to stripper. After stripped by steam, the spent catalyst is removed to a regenerator where it is contacted with an oxygen containing gas and is regenerated, the hot regenerated catalyst is stripped and then recycled to the reactor for reuse. (1) The Catalyst Catalyst used in the present invention is consisting of 0-70% by weight of clay, 5-90% by weight of inorganic oxides and 10∼35% by weight of zeolites. Wherein said clay is selected from kaolin andlor halloysite, said inorganic oxide is selected from SiO 2 · Al 2 O 3 , SiO 2 and/or Al 2 O 3 , said zeolite components comprising 25-100% by weight of phosphorus and rare earth containing high silica zeolite having a structure of pentasil, 0-75% by weight of high silica Y type zeolite and 0-25% by weight of rare earth containing Y type zeolite. High silica Y type zeolite used in the present invention is high SilAl ratio, stabilised high silica Y type zeolite with rare earth content of 0-3% by weight (calculated as RE 2 O 3 ) treated with various chemical and/or physical methods, such as hydrothermal method, acid treating method, framework silicon enriching method, and SiCl 4 treatment method. Rare earth containing Y type zeolite used in the present invention is selected from rare earth exchanged Y type zeolite (REY) and/or rare earth-hydrogen-containing Y type zeolite (REHY). Phosphorus and rare earth containing high silica zeolite having a structure of pentasil (designated as P-ZRP hereinafter) used in the present invention is a rare earth containing high silica zeolite having a structure of pentasil modified by aluminium phosphate, with a phosphorus content of 2-20% by weight (calculated as P 2 O 5 ), preferably 2-10% by weight. Above said rare earth containing high silica zeolite having a structure of pentasil (commercial name ZRP) is prepared according to the method disclosed in U.S.Pat.No.5,232,675 or EP 0550917 A, using water glass, aluminium phosphate and inorganic acid as raw materials, and KEY or BEHY zeolite as crystalline seeds, and is crystallised at 130-200° C for 12-60 hours. ZRP zeolite possesses an X-ray diffraction pattern of ZSM-5 zeolite family and an anhydrous chemical composition formula: 0.01-0.30 RE 2 O 3 0.4-1.0 Na 2 O · Al 2 O 3 20-60 SiO 2 , in where, the rare earth comes from the seeds used for the synthesis of ZRP zeolite. ZRP zeolite has a 2-4 times higher adsorption capacity ratio of normal hexane to cyclohexane adsorption than that of ZSM-5 zeolite. ZRP zeolite was modified by aluminium phosphate as follows: the zeolite was pre-exchanged with ammonium ion to decrease its sodium content to a level of not more than 0.1% by weight (calculated as Na 2 O), then mixed homogeneously ith an aluminium phosphate sol having a composition of Al 2 O 3 : P 2 O 5 =1 : 1-3 according to a weight ratio of P 2 O 5 : zeolite (anhydrous basis) = 1 : 5-99, followed by calcining at 300-600° C for 0.5-6 hours in the presence of 10-100% steam. (2) The Feed Hydrocarbon feedstocks in accordance with the present invention, which may vary in a wide range, comprise petroleum fractions with different boiling ranges, such as naphtha, distillate, vacuum gas oil, residual oil and the mixture thereof. Crude oil may also be directly used. The pattern of feed injection into reactor can use single point injection or multi-point injection. (3) Process and Operating Conditions thereof The process provided by the present invention comprises: petroleum hydrocarbons are preheated and then injected into the riser or downflow transfer line reactor or fluidized bed reactor, in where petroleum hydrocarbons are contacted with hot phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts and catalytically converted at a temperature of 480° to 680° C, preferably from 500° to 620° C, a pressure of 1.2×10 5 to 4.0 × 10 5 Pa, with a contact time of 0.1 to 6 seconds, preferably from 0.1 to 5 seconds, a weight ratio of catalyst to feedstock of 4:1 to 20:1, preferably from 5:1 to 15:1 and a weight ratio of steam to feedstock of 0.01:1 to 0.5:1, preferably from 0.05:1 to 0.3:1. The reaction effluent, steam and spent catalyst are separated by rapid gas-solid separation, the reaction effluent is continuously separated to obtain light olefins including ethylene, propylene, isobutylene, isoamylene, etc. and liquid products, and the spent catalyst is continuously removed to stripper. After stripped by steam and/or other gas, hydrocarbon products which are adsorbed on the catalysts are stripped out. The spent catalyst with coke deposited thereon is then removed to a regenerator. Regeneration is conducted by contacting the catalyst with an oxygen-containing gas, such as air, at a temperature of 600° to 800° C. After stripped by steam and/or other gas, the hot regenerated catalyst is recycled to the reactor for reuse. Hot regenerated catalyst supplies catalytic conversion of petroleum hydrocarbon with the needed reactive heat. And after reaction the spent catalyst is regenerated in the regenerator to emit heat which will be absorbed by the regenerated catalyst. After the regenerated catalyst is returned to reactor, it further supplies the catalytic conversion of petroleum hydrocarbons with the absorbed heat. The advantages of the present invention are as follows: 1. In a comparison with conventional catalytic cracking processes, the process provided by the present invention uses phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts with lower hydrogen transfer activity and higher olefin selectivity, thus increases the yields of light olefins, especially propylene,isobutylene and isoamylene. 2. In a comparison with prior catalytic conversion processes for producing light olefins, the process provided by the present invention uses dilute phase transfer line reactor and phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalyst with higher cracking activity and higher olefin selectivity, thus increases the yields of light olefins, especially propylene, isobutylene and isoamylene. 3. The process of the present invention provides the suitable catalysts, reactor model and operating conditions, thus obtains higher yields of light olefins, especially isoolefins, wherein isobutylene yield is 6.57% by weight and isoamylene yield is 6.52% by weight. 4. The feedstocks used in the process of the present invention possess very wide boiling ranges, may comprise petroleum fractions with different boiling ranges,such as naphtha, distillate, vacuum gas oil, residual oil and the mixture thereof, crude oil may also be directly used. The following examples will serve to further illustrate the catalytic conversion process provided by the present invention. However, these examples are not to be construed to limit the scope of the present invention. The main properties of feedstocks used in the following examples are listed in Table 1. Feedstock A B C D E F G Crude oil Density (20°C), g/ml .881 .904 .856 .923 .726 .816 .873 .857 Conradeon carbon, wt% 0.26 0.16 0.22 0.35 - - 4.78 3.54 Basic nitrogen, ppm 537 585 420 683 - - 837 623 Ni content, ppm 0.08 1.41 0.49 3.62 - - 8.92 6.28 V content, ppm 0.01 0.05 0.03 0.45 - - 0.72 0.50 UOP K factor 12.0 11.8 - 11.4 - - - - Distillation range, °C 256-545 243-507 319-504 241-540 54-228 235-364 >346 - The catalysts used in these examples are as follows: Catalyst A was prepared according to the method of example 3 disclosed in U.S. Ser. No.08/072,771 (filed on June 7,1993) or Netherland Ser. No.9301333. It was consisting of 15.0% by weight of P-ZRP zeolite, 59.5% by weight of kaolin and 25.5% by weight of Al 2 O 3 . Catalyst B was prepared according to the method of example 5 disclosed in U.S.Ser.No.08/072,771 (filed on June 7, 1993) or Netherland Ser. No.9301333. It was consisting of 18.0% by weight of P-ZRP zeolite and balance amounts of amorphous aluminosilicate (SiO 2 · Al 2 O 3 ). Catalyst C was prepared according to the method of example 7 disclosed in U.S.Ser.No.08/072,771 (filed on June 7, 1993) or Netherland Ser. N.9301333. It was consisting of 16.1% by weight of P-ZRP zeolite, 1.8% by weight of REY zeolite, 57.4% by weight of kaolin and 24.6% by weight of Al 2 O 3 . Catalyst D was prepared according to the preparation method of conventional semi-synthetic cracking catalyst. It was consisting of 12.0% by weight of P-ZRP zeolite, 8% by weight of REUSY zeolite (wherein RE 2 O 3 content ≤ 3% by weight), 54.5% by weight of kaolin and 25.5% by weight of Al 2 O 3 . Catalyst E was prepared according to the preparation method of conventional semi-synthetic cracking catalyst. It was consisting of 10% by weight of P-ZRP zeolite, 10% by weight of USY zeolite, 2% by weight of KEY zeolite, 59.3% by weight of kaolin and 18.7% by weight of Al 2 O 3 . Catalyst F was prepared according to the preparation method of conventional semi-synthetic cracking catalyst. It was consisting of 10.0% by weight of P-ZRP zeolite, 10.0% by weight of high silica Y type zeolite (prepared with liquid phase framework silicon enriching method), 2.0% by weight of KEY zeolite, 59.3% by weight of kaolin and 18.7% by weight of Al 2 O 3 . Catalyst G was prepared according to the preparation method of conventional semi-synthetic cracking catalyst. It was consisting of 8.0% by weight of P-ZRP zeolite, 8.0% by weight of REUSY zeolite, 4.0% by weight of USY zeolite, 56.5% by weight of kaolin and 23.5% by weight of Al 2 O 3 and SiO 2 . Example 1 This example illustrates the process provided by the present invention for producing light olefins by using single zeolite (P-ZRP) containing catalyst with semi-synthetic matrix. The catalytic conversion was carried out in a bench scale fixed-fluidized bed reactor with Feedstock A and Catalyst A at the temperature of 580° C and the pressure of 1.3×10 5 Pa, with the contact time of 5 seconds, the weight ratio of catalyst to feedstock of 5:1 and the weight ratio of steam to feedstock of 0.2:1. The results of the test were listed in Table 2. (Comparative Example 1) H-ZSM-5 zeolite was used instead of P-ZRP zeolite to prepare a catalyst as Comparative Sample 1, the catalyst was used in U.S.Pat.No.4,980,053 or EP No.305,720A. Table 2 also lists the results of the test with Comparative Sample 1 at the same operating conditions as Example 1. The results in Table 2 show that: under the same operating conditions, the process provided by the present invention displayed in higher yields of light olefins, especially propylene, isobutylene and isoamylene than the prior art (U.S.Pat.No.4,980,053 or EP No.305,720 A). Catalyst A Comparative Sample 1 Product Yield, wt% Cracking gas 51.02 43.81 Wherein, ethylene 6.16 4.36 propylene 19.74 16.70 total butylene 13.71 12.52 isobutylene 5.92 5.18 Gasoline (C 5 ∼221° C) 28.80 30.64 Wherein, total amylene 5.38 4.63 isoamylene 3.62 3.08 Diesel (221∼330° C) 6.60 7.34 Bottoms (>330° C) 7.22 11.99 Coke 6.36 6.22 Conversion, wt% 86.18 80.67 C 2 ∼C 5 olefins, wt% 44.99 38.21 Isobutylene plus isoamylene, wt% 9.54 8.26 Example 2 This example illustrates the process provided by the present invention for producing light olefins by using single zeolite ( P-ZRP) containing catalyst with full-synthetic matrix. The catalytic conversion was carried out in a bench scale fixed-fluidized bed reactor with Feedstock A and Catalyst B at the same operating conditons as Example 1. The results of the test are listed in Table 3. Catalyst B Product Yield, wt% Cracking gas 55.30 Wherein, ethylene 6.20 propylene 18.32 total butylene 13.11 isobutylene 5.38 Gasoline (C 5 ∼221° C) 26.50 Wherein, total amylene 4.90 isoamylene 3.25 Diesel (221∼330° C) 7.77 Bottoms (>330° C) 3.65 Coke 6.78 Conversion, wt% 88.58 C 2 ∼C 5 olefins, wt% 42.53 Isobutylene plus isoamylene, wt% 8.63 Example 3 This example illustrates the process provided by the present invention for producing light olefins by using dual zeolites (P-ZRP and REY) containing catalyst. The catalytic conversion was carried out in a bench scale fixed-fluidized bed reactor with Feedstock B and Catalyst C at the same operating conditions as Example 1. The results of the test are listed in Table 4. (Comparative Example 2) H-ZSM-5 zeolite was used instead of P-ZRP zeolite to prepare the catalyst as Comparative Sample 2, the catalyst was used in U.S.Pat.No.4,980,053 or EP No.305,720A. Table 4 also lists the results of the test with Comparative Sample 2 at the same operating conditions as Example 3. The results in Table 4 show that: under the same operating conditions the process provided by the present invention possessed in higher yields of light olefins, especially propylene, isobutylene and isoamylene than the prior art (U.S.Pat.No. 4,980,053 or EP No.305,720 A). Catalyst C Comparative Sample 2 Product Yield, wt% Cracking gas 49.24 41.54 Wherein, ethylene 5.32 2.85 propylene 18.31 15.48 total butylene 13.47 12.36 isobutylene 5.49 4.99 Gasoline (C 5 ∼221° C) 27.61 28.62 Wherein, total amylene 4.99 4.58 isoamylene 3.32 3.02 Diesel (221∼330° C) 7.32 9.94 Bottoms (>330° C) 8.22 12.45 Coke 7.61 7.45 Conversion, wt% 84.46 77.61 C 2 ∼C 5 olefins, wt% 42.09 35.27 Isobutylene plus isoamylene, wt% 8.81 8.01 Example 4 This example illustrates the process provided by the present invention for producing light olefins by using P-ZRP zeolite, USY zeolite and REUSY zeolite containing catalyst. The catalytic conversion was carried out in a bench scale fixed-fluidized bed reactor with Feedstock B and Catalyst G at the temperature of 500° C and the pressure of 1.4×10 5 Pa, with the contact time of 1.5 seconds, the weight ratio of catalyst to feedstock of 6:1 and the weight ratio of steam to feedstock of 0.05:1. The results of the test are listed in Table 5. Catalyst G Product Yield, wt% Cracking gas 42.15 Wherein, ethylene 3.45 propylene 14.14 total butylene 10.28 isobutylene 4.31 Gasoline (C 5 ∼221° C) 39.70 Wherein, total amylene 5.27 isoamylene 3.68 Diesel (221∼330° C) 8.53 Bottoms (>330° C) 4.57 Coke 5.05 Conversion, wt% 86.90 C 2 ∼C 5 olefins, wt% 33.14 Isobutylene plus isoamylene, wt% 7.99 Example 5 This example illustrates the process provided by the present invention for producing light olefins by using triple zeolite(P-ZRP, high silica Y type and REY) containing catalyst. The catalytic conversion were carried out in a bench scale fixed-fluidized bed reactor with Feedstock C and Catalyst E and F at the temperature of 515° C, with the weight space velocity of 14 per hour, the weight ratio of catalyst to feedstock of 8:1 and the weight ratio of steam to feedstock of 0.07:1. The results of the tests are listed in Table 6. (Comparative Example 3) H-ZSM-5 zeolite was used instead of P-ZRP zeolite to prepare the catalyst as Comparative Sample 3, the catalyst was used in CN No.1072203 A. Table 6 also lists the results of the test with Comparative Sample 3 at the same operating conditions as Example 5. The results in Table 6 show that: under the same operating conditions the process provided by the present invention possessed in higher yields of light olefins, especially isoolefins than the prior art (CN No.1072203 A). Catalyst E Catalyst F Comparative Sample 3 Product Yield, wt% Cracking gas 40.64 42.28 33.10 Wherein, ethylene 2.59 2.63 0.91 propylene 13.63 14.25 9.75 total butylene 11.53 12.38 7.45 isobutylene 4.95 5.33 2.53 Gasoline ( C 5 ∼221°C) 41.63 40.45 47.00 Wherein, total amylene 6.29 6.42 - isoamylene 4.38 4.51 - Diesel (221∼330°C) 9.27 9.12 9.20 Bottoms ( >330°C ) 4.82 4.63 5.30 Coke 3.64 3.52 5.40 Conversion, wt% 85.91 86.25 85.50 C 2 ∼C 4 olefins, wt% 27.75 29.26 18.11 Isobutylene plus isoamylene, wt% 9.33 9.84 - Example 6 This example illustrates the process provided by the present invention for production of light olefins by catalytic conversion of petroleum hydrocarbons in riser reactor. The test was carried out on a pilot riser unit with continuous reaction and regeneration operation system using Feedstock A and Catalyst D and operated in the single pass operation mode. The feedstock was preheated to about 350° C and then injected into the inlet of riser reactor, steam with high temperature was injected to the outlet of preheater and the inlet of riser reactor, the weight ratio of steam to feedstock was 0.1:1. The feedstock was contacted with heated catalyst in riser reactor and catalytically converted at riser reactor outlet temperature of 530° C and the pressure of 1.7×10 5 Pa with the contact time of 2.3 seconds and the weight ratio of catalyst to feedstock of 10:1. Reaction effluent, steam and spent catalyst were separated by rapid gas-solid separation in the outlet of riser reactor, reaction effluent was continuously separated to obtain light olefins including ethylene, propylene, isobutylene and isoamylene and liquid products, and spent catalyst was continuously removed to the stripper. After stripped by steam, the spent catalyst was removed to a regenerator where it was contacted with an oxygen containing gas and was regenerated, the hot regenerated catalyst was stripped and then recycled to the reactor for reuse. The results of the test are listed in Table 7. The data in Table 7 show that: the process provided by the invention under catalytic cracking conditions possessed obviously higher isoolefin yields than conventional catalytic cracking process, in where isobutylene yield was 6.57% by weight and isoamylene yield was 6.52% by weight, besides, high octane gasoline with MON 82.0 and RON 95.4 was produced. Catalyst D Product Yield, wt% Cracking gas 35.93 Wherein, ethylene 2.52 propylene 12.45 total butylene 15.71 isobutylene 6.57 Gasoline (C 5 ∼221° C) 40.98 Wherein, total amylene 9.41 isoamylene 6.52 Diesel (221∼330° C) 12.06 Bottoms (>330° C) 6.64 Coke 4.39 Conversion, wt% 81.30 C 2 ∼C 5 olefins, wt% 40.09 Isobutylene plus isoamylene, wt% 13.09 Gasoline properties MON 82.0 RON 95.5 Example 7 This example illustrates that vacuum gas oil derived from various crude oils can be used as feedstock in the process provided by the present invention for producing light olefins. The tests were carried out in a bench scale fixed-fluidized bed reactor by using Catalyst E at the temperature of 515° C, with the contact time of 1 second, the weight ratio of catalyst to feedstock of 8:1 and the weight ratio of steam to feedstock of 0.05:1. The results of the tests are listed in Table 8. Feedstock A Feedstock B Feedstock D Product Yield, wt% Cracking gas 44.09 42.93 37.32 Wherein, ethylene 3.26 3.05 2.21 propylene 15.05 14.35 12.28 total butylene 11.02 10.06 9.41 isobutylene 4.72 4.38 3.95 Gasoline (C 5 ∼221° C) 40.57 39.46 37.66 Wherein, total aamylene 6.06 5.51 5.03 isoamylene 4.25 3.83 3.48 Diesel (221∼330° C) 6.64 7.56 11.35 Bottoms (>330° C) 2.96 4.12 7.28 Coke 5.74 5.93 6.39 Conversion, wt% 90.40 88.32 81.37 C 2 ∼C 5 olefins, wt% 35.39 32.97 28.93 Isobutylene pllus isoamylene, wt% 8.97 8.21 7.43 Example 8 This example illustrates that hydrocarbons with different boiling ranges can be used as feedstock in the process provided by the present invention for producing light olefins. The tests were carried out in a bench scale fixed-fluidized . bed reactor by using Catalyst A. The operating conditions and the results of the tests are listed in Table 9. Feedstock E Feedstock F Feedstock G Crude oil Operating conditions Temperature, °C 680 650 580 580 Contact time, seconds 0.5 0.1 6 5 Catalyst/oil, wt/wt 20:1 16:1 4:1 6:1 Steam/oil, wt/wt 0.15:1 0.01:1 0.5:1 0.3:1 Product Yield, wt% Cracking gas 52.72 39.54 49.98 43.77 Wherein, ethylene 11.87 4.89 5.61 4.36 propylene 13.94 15.38 19.21 16.36 total butylene 10.52 8.78 14.56 12.47 isobutylene 3.58 3.48 5.82 5.03 Gasoline ( C 5 ∼221°C) 43.59 40.27 25.18 33.35 Wherein, total amylene 4.77 4.46 5.71 4.72 isoamylene 3.09 2.87 3.80 3.12 Diesel (221∼330°C) 0.23 16.77 9.35 9.71 Bottoms ( >330°C ) 0.00 0.04 6.84 4.48 Coke 3.46 3.38 8.65 8.69 Conversion, wt% 99.77 83.19 83.81 85.81 C 2 ∼C 5 olefins, wt% Isobutylene plus 41.10 33.51 45.09 37.91 isoamylene, wt% 6.67 6.35 9.60 8.15

Claims: A process of catalytic conversion of petroleum hydrocarbons comprises: preheated hydrocarbons are contacted with phosphorus and rare earth containing high silica zeolite having a structure of pentasil catalysts in the moving catalyst reactor and catalytically converted at a temperature of 480° to 680° C and a pressure of 1.2×10 5 to 4×10 5 Pa, with a contact time of 0.1 to 6 seconds, a weight ratio of catalyst to feedstock,of 4:1 to 20:1 and a weight ratio of steam to feedstock of 0.01:1 to 0.5:1. The process of Claim 1, wherein said catalytic conversion is carried out at a temperature of 500° to 620° C, with a contact time of 0.1 to 6 seconds, a weight ratio of catalyst to feedstock of 5:1 to 15:1 and a weight ratio of steam to feedstock of 0.05:1 to 0.3:1. The process of Claim 1, wherein said moving catalyst reactor is a riser reactor. The process of Claim 1, wherein said moving catalyst reactor is a downflow transfer line reactor. The process of Claim 1, wherein said moving catalyst reactor is a fluidized bed reactor. The process of Claim 1, wherein said catalyst is consisting of 0-70% by weight of clay which is selected from kaolin and/or halloysite, 5-90% by weight of inorganic oxides which are selected from SiO 2 · Al 2 O 3 , SiO 2 and/or Al 2 O 3 and 10∼35% by weight o f zeolites. The process of Claim 6, wherein said zeolite components comprise 25-100% by weight of phosphorus and rare earth containing high silica zeolite having a structure of pentasil, 0-75% by weight of high silica Y type zeolites and 0-25% by weight of rare earth containing Y type zeolites. The process of Claim 7, wherein said high silica Y type zeolite is stabilised high silica Y type zeolite with rare earth content of 0-3% by weight (calculated as RE 2 O 3 ) treated with various chemical andlor physical methods to obtain a high Si/Al ratio. The process of Claim 7, wherein said rare earth containing Y type zeolite is selected from rare earth exchanged Y type zeolite andlor rare earth-hydrogen containing Y type zeolite. The process of Claim 7, wherein said phosphorus and rare earth containing high silica zeolite having a structure o f pentasil is a rare earth containing high zeolite having a structure of pentasil treated with aluminium phosphate, possessing a phosphorus content of 2-20% by weight (calculated as P 2 O 5 ). The process of Claim 7, wherein said phosphorus and rare earth containing high silica zeolite having a structure o f pentasil is a rare earth containing high silica zeolite having a structure of pentasil treated with aluminium phosphate, possessing a phosphorus content of 2-10% by weight (calculated as P 2 O 5 ). The process of Claim 10, wherein said rare earth containing high silica zeolite having a structure of pentasil possesses an X-ray diffraction pattern of ZSM-5 zeolite family and an anhydrous chemical composition formula: 0.01-0.30 RE 2 O 3 · 0.4-1.0 Na 2 O Al 2 O 3 20-60 SiO 2 , in where the rare earth comes from the seeds used for the synthesis of the zeolite, and a 2-4 times higher adsorption capacity ratio of normal hexane t o cyclohexane adsorption than that of ZSM-5 zeolite. The process of Claim 10, wherein said rare earth containing high silica zeolite having a structure of pentasil is prepared by using water glass, aluminium phosphate, and inorganic acid as raw materials, and KEY or REHY zeolite as crystalline seeds, and was crystallised at 130° -200° C for 12-60 hours. The process of Claim 10, wherein said treatment procedure of rare earth containing high silica zeolite having a structure of pentasil is pre-exchanged with ammonium ion to decrease its sodium content to a level of not more than 0.1% by weight (calculated as Na 2 O), then mixed homogeneously with an aluminium phosphate sol having a composition of Al 2 O 3 :P 2 O 5 = 1:1-3 according to a weight ratio of P 2 O 5 :zeolite (anhydrous basis)=1:5-99, followed by calcining at 300-600° C for 0.5-6 hours in the presence of 10-100% steam. The process of Claim 1, wherein said hydrocarbon feedstocks comprise petroleum fractions with different boiling ranges, such as naphtha, distillate, vacuum gas oil, residual oil and the mixture thereof as well as crude oil. The process of Claim 1, wherein the pattern of feed injection into reactor is single point injection or multi-point injection. The process of Claim 1, which further comprises that the reaction effluent is separated to obtain light olefins and liquid products, spent catalyst is stripped and then removed to a regenerator where it is contacted with an oxygen containing gasat a temperature of 600° to 800° C and is regenerated, the regenerated catalyst is stripped and then recycled to the reactor for reuse. Use of the process of claim 1 for producing light olefins. Use of the process of claim 1 for producing ethylene, propylene, isobutylene and isoamylene. Use of the process of claim 1 for producing high octane gasoline

Inventors: JIANG FUKANG, LI SHICHUN, LI ZAITING, LIU SHUNHUA, PAN RENNAN, SHI WENYUAN, XIE CHAOGANG, JIANG, FUKANG, LI, SHICHUN, LI, ZAITING, LIU, SHUNHUA, PAN, RENNAN, SHI, WENYUAN, XIE, CHAOGANG
Applicants: CHINA PETROCHEMICAL CORP, RES INST PETROLEUM PROCESSING, CHINA PETRO-CHEMICAL CORPORATION, RESEARCH INSTITUTE OF PETROLEUM PROCESSING, SINOPEC
Application year: 1994
Main classification: C10G11
IPC codes: C07B61, C07C4, C10G49, C07C11, B01J29, C10G11, C10G35